Gold-containing catalyst with porous structure

ABSTRACT

The invention relates to a gold-containing catalyst with porous structure that is obtainable through a process that comprises the following steps: melting together of gold and at least one less noble metal that is selected from the group consisting of silver, copper, rhodium, palladium, and platinum, and at least partial removal by dissolving the at least one less noble metal out of the starting alloy thus obtained. The catalyst has high activity and great long-term stability, despite the fact that it does not contain a support material or a compound that serves as a support material. The catalyst can be used to accelerate and/or to influence the product selectivity of oxidation and reduction reactions. The catalyst is suitable, for example, for the oxidization of carbon monoxide to carbon dioxide, which makes it usable, among other things, in a fuel cell, in particular a polymer electrolyte membrane fuel cell (PEM), for protection of the anode catalyst against blocking by carbon monoxide.

The United States Government has rights in this invention pursuant toContract No. W-7405-ENG-48 between the United States Department ofEnergy and the University of California for the operation of LawrenceLivermore National Laboratory.

FIELD OF INVENTION

The present invention relates to a gold-containing catalyst with porousstructure, the use of the catalyst according to the invention toaccelerate and/or influence the product selectivity of oxidation andreduction reactions, as well as a fuel cell with a catalyst according tothe invention.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application claims the benefit of German Patent Application No.XXXXXXXXXX, filed Mar. 27, 2006 and titled “GOLD-CONTAINING CATALYSTWITH POROUS STRUCTURE” is incorporated herein by this reference.

The action of catalysts is known to be based on the fact that they opena path to chemical reactions by which starting compounds or materialscan be converted into end products by application of a small activationenergy. However, catalysts not only accelerate a chemical reaction inthis manner, but they can frequently also influence the objective of thereaction. Consequently, catalysts have immense significance in allfields in which an accelerated or targeted chemical conversion of eductsis desirable or necessary.

Gold-based catalysts have been known for only a few years. They aresuitable for both oxidation and reduction reactions, with the focus ofthe research and application fields certainly concentrating on the fieldof oxidation reactions. In this area, gold-containing catalysts areknown, for example, for oxidation of ethylene and acetic acid to vinylacetate or the partial or selective oxidation of hydrocarbons. However,the best-known application for gold-based catalysts has to be theoxidation of carbon monoxide to carbon dioxide. This reaction is oftenused not only as a model for investigation of the activity andproperties of gold-based catalysts; such catalysts are among the fewsystems with which this reaction can already occur to an extent worthmentioning at room temperature.

In the area of reduction reactions, the use of gold-based catalysts hasbeen described, for example, in the hydrogenation of carbon monoxide,carbon dioxide, and acetylene. Furthermore, gold catalysts in the formof supported gold particles have also been investigated with verypositive results for applications in the reduction of nitrogen oxides aswell as for hydrogenation reactions of alkenes or unsaturated aldehydes.(Masatake Haruta, CatTech, 2002, 6, 102415; Masatake Haruta, Cat, Today,1997, 36, 153-166.)

It is further known that gold, as the most noble metal, can have acatalytic effect only under certain conditions. One of these conditionsis, for example, that the gold must be present in very small (nano)particles. Such very small gold particles have, however, large surfaceenergy and, consequently, tend to coagulate quickly, as a result ofwhich their catalytic activity is greatly reduced.

For this reason, it has been proposed, to immobilize gold (particles) ona support material, in particular a transition metal oxide. A group ofprocesses for the production of such catalytically activegold-containing systems are known that are directed at positivelyinfluencing the parameters important for catalytic systems, such as, forinstance, selectivity, the reaction conditions (such as pressure andtemperature) necessary for the progress of catalytic reactions, reactionspeeds obtainable, as well as long-term stability, for example, throughthe use of new support materials or through the use of new processes forthe production of gold and/or support material particles.

Thus, it has been proposed, for instance, in DE 4238640 A1 to producethe metal oxide with immobilized gold by means of mixed precipitation,wherein, however, part of the gold is located inactively in the interiorof the resulting particles.

In order to circumvent this disadvantage, it has been proposed,repeatedly, to supply the gold to already existing porous supportparticles. Accordingly, WO 00/64581 teaches, for example, to firstproduce a particle of titanium-silicon mixed oxide using a sol-gelprocess; and then to deposit the gold on it using known processes, suchas precipitation, impregnation, spluttering, chemical vapor deposition(CVD), or physical vapor deposition.

When gold is used in dissolved form (e.g., as AuCl₃) to deposit it, forexample, by impregnation on the surface of support particles, as isproposed among other things in WO 03/106021, it is necessary totransform the gold cations into metallic form through an additionalreduction reaction.

With wet chemical processes, problems related to reproducibility of thechemical/physical properties of the catalytic systems obtained arereported. These difficulties probably are based, for example, on thefact that, among other things, it is difficult to control the size ofthe gold particles, that the catalysts are poisoned by ions such as, forexample, chloride, that different amounts of gold “get lost” in thepores of the support material, and that, through necessary thermalsecondary processing steps, the catalytic activity of the material isaltered in a non-reproducible manner.

For this reason, it is proposed, e.g., in WO 2005/03082 to deposit thegold by PVD on support material particles. A suitable vacuum apparatusis required for the PVD process, which makes the process expensive interms of equipment and also imposes restrictions with regard to the sizeand shape of the support material used.

WO 03/059507 describes gold-containing catalytic materials that areproduced by melting gold and a less noble metal together and then atleast partially removing the less noble metal from the material obtainedthrough chemical or electrochemical treatment. The metals of the groupsIIB (Zn, Cd, Hg) and IIIA (B, Al, Ga, In, Tl) are proposed as less noblemetals. It is further proposed to additionally provide a metal from oneof the groups IVB, VB, VIB, VIII, IB, IIB, IIIA, IVA, as well asmagnesium and cerium as a promoter. Also, in WO 03/059507 it is assumedthat the finished catalyst has to have a support material based on ametal oxide since that is the only way to be able to prevent rapidagglomeration and sintering of the gold-containing material.

From this brief overview of known processes for the production ofgold-containing catalysts, it is clear that, in each case, multiplecomplex and/or expensive steps are required before obtaining agold-containing catalyst usable in practice.

Consequently, one object of the present invention is to provide agold-containing catalyst with which the disadvantages known from theprior art are reduced. Another object of the present invention is toprovide advantageous applications for the catalyst according to theinvention.

SUMMARY OF THE INVENTION

These objects are accomplished through a gold-containing catalyst withporous structure, prepared by a method that includes the followingsteps: producing a starting alloy by melting together of gold and atleast one less noble metal that is selected from the group consisting ofsilver, copper, rhodium, palladium, and platinum; and a dealloying stepincluding at least partial removal of the less noble metal by dissolvingthe at least one less noble metal out of the starting alloy. It isdesirable that the resulting gold-containing catalyst with porousstructure contains no support structure for the gold.

The catalyst can be used advantageously in a process to accelerateand/or influence the product selectivity of oxidation and reductionreactions, and more particularly in a fuel cell.

The gold-containing catalyst with porous structure according to theinvention is characterized in that it is obtainable through a processthat comprises the following steps: melting together of gold and atleast one less noble metal that is selected from the group consisting ofsilver, copper, rhodium, palladium, and platinum, and at least partialremoval by dissolving the at least one less noble metal out of thestarting alloy thus obtained. The preferred less noble metals for use inthis invention include silver, copper and palladium, with silver beingmost preferred. The step of the at least partial dissolving out of theat least one less noble metal from the starting alloy is referred tohereinafter as a “dealloying process.”

The catalyst according to the invention is surprisingly distinguished byhigh activity and great long-term stability, despite the fact that itdoes not contain a support material or a compound (e.g., a transitionmetal oxide) that serves as a support material. This is all the moresurprising since all prior art assumed that such a support material isabsolutely necessary in order to obtain adequate catalytic activity andstability of a gold-based catalyst.

DETAILED DESCRIPTION

The production of a gold-containing starting alloy is known to theperson skilled in the art and may occur, for example, through simplemixing of the metals in a desired quantitative proportion and subsequentmelting of the metals in a furnace, optionally in a protective gasatmosphere.

Starting alloys in which the ratio of gold to the less noble metal(s) isin the range from 50 atom %: 50 atom % to 10 atom %: 90 atom % aresuitable for the catalyst according to the invention.

In the case of a gold-silver starting alloy (Au—Ag-starting alloy), thecomposition can be within the range from 20 to 45 atom %, i.e., at aratio of gold to silver in the range from 45 atom % 55 atom % to 20 atom%: 80 atom %. In the case of an Au—Ag-starting alloy, higherAu-concentrations result in the formation of a passivation layer andlower Au-concentrations do not yield a monolithic porous metal body. Thepossible concentration limits for each alloy type for all the metalsdisclosed herein can be readily determined by a person skilled in theart. For the measurements of catalytic activity described below, anAu—Ag-starting alloy with 30 atom % Au was used.

Within the respective possible concentration limits, additionaloptimization may be undertaken. What is considered optimal in eachindividual case may differ; accordingly, for example, optimization mayhave as its goal the highest possible activity, the longest possibleservice life, or even the least possible cost.

After the production of the starting alloy, it is advantageous tohomogenize the starting alloy. This is achieved by holding the startingalloy for an adequate time at a temperature just below the meltingpoint.

One of the particular advantages of the catalyst according to theinvention is that its production starts from a starting alloy. Thestarting alloy obtained can be given almost any shape before thedealloying process, and, thus, virtually any desired shape can beobtained. The external shape of the starting alloy is not altered by thedealloying process described below, such that the shape of the latercatalyst can already be predefined through the shaping of the startingalloy.

Any suitable process can be used for the shaping of the starting alloy,such as, pressing, stamping, rolling, bending, boring, hammering,cutting, and/or milling. Since these methods are usually notparticularly expensive from a technical standpoint (for example, novacuum chamber is required), virtually any desired size and shape of thecatalyst can be produced simply and cost-effectively.

The shaped starting alloy is preferably annealed before the dealloyingprocess in order to reduce mechanical stresses, for 24 hours at 850° C.,for example.

The starting alloy may, however, for example, also be given a desiredshape or an advantageous shape for additional processing or shapingusing a casting process. If the shaping of the catalyst according toinvention occurs exclusively by means of a casting process, the startingalloy obtained is advantageously merely homogenized.

The at least partial dealloying and creation of the porous structurethen occurs in a next step preferably through the use of at least oneelectrochemical and/or wet-chemical process. Which process or whichcombination of different processes is the most suitable in each casedepends, among other things, on the composition of the alloy and/or theintended use of the resultant catalyst. The most suitable process or themost suitable combination can be determined by a person skilled in theart through a few experiments.

With the use of an electrochemical process, the partial or completedealloying of the less noble metal out of the starting alloy and theextent of the dealloying (i.e., how much of the less noble metal isstill found or remains in the starting alloy) can be very preciselycontrolled by adjusting the voltage or current density of the electricalprocess.

For example, the silver portion can be dissolved out of theAu—Ag-starting alloys to the extent desired by fixing the specimensusing a gold plated clamp and placing them, for example, in a solutionwith 1 M HNO₃ and 0.01 M AgNO₃. The solution described is appropriatefor a silver pseudo-reference electrode, but must not be used forsilver/silver chloride reference electrodes. In the latter case, therewould be a risk of contamination of the solution with chloride ions. Inorder to free the starting alloy of silver, voltage above the criticalpotential is applied. The dealloying process is terminated when theelectrical current drops into the range of a few microamperes. Then, thespecimen is usually washed several times with water and then dried inair. The residual proportion of the at least one less noble metal can becontrolled by the total current conducted or the conditions at the endof the electrolysis.

An at least partial dealloying occurs through the use of a wet-chemicalprocess using a solution with a composition such that it causesdissolution of the less noble metal out of the starting alloy. Thecomposition of the solution is guided by the requirement of being ableto dissolve the less noble metal(s) but without significantly attackingthe gold in the starting alloy.

One example of such a solution for the at least partial dealloying of anAu—Ag-starting alloy with 30 atom % gold consists in a solution of 70%nitric acid. With such a solution, it is possible, for example, to(partially) dealloy 300 μm thick specimens within one to three days atroom temperature. At least the majority of the silver portion isselectively dissolved out of specimens by nitric acid, and nanoporousgold foams remain. The acid is removed by washing the specimens severaltimes with water; then, the specimens can be dried in air.

The proportion of the less noble metal(s) can be expediently reduced tothe desired remainder through process control during the dealloyingprocess, with this remainder being as low as a proportion of 0 atom %.

The material has, after partial or complete dealloying, a ratio of goldto the at least one less noble metal in the range from 100 atom %: 0atom % to roughly 95 atom %: 5 atom %. These data are based on resultsof analyses using atom absorption spectroscopy (AAS), with which theentire composition of the material can be determined.

Analyses using XPS (XPS=X-ray photoelectron spectroscopy) yielded ratiosof gold to the at least one less noble metal in the same materials inthe range from roughly 100 atom %: 0 atom % to roughly 80 atom %: 20atom %. To the extent the values determined using XPS indicated a higherproportion for the at least one less noble metal, this is based on thefact that XPS is a highly surface sensitive measurement method. It iswell known to the individuals skilled in the art that in alloys one ormore metals may be enriched on the surface relative to the interior.

The optimum proportion of the less noble metal that should remain in theporous gold-containing catalyst for the respective desired purpose maybe determined simply by an individual skilled in the art by experiment.As already explained above with regard to the mix ratio of the metalsfor the starting alloy, there is also the possibility with regard to theresidual metal content of the less noble metal that the question as towhat is considered optimum can be answered differently for eachapplicational case; here again, optimization may, for example, have asits goal the highest possible activity, the longest possible servicelife, an optimum degree of porosity, or even the least possible cost.

In order for the catalyst according to the invention to develop its fullcatalytic activity, it is activated advantageously by a moderatelyelevated temperature (e.g., in the range from roughly +40 to +80° C.) inan oxygen-containing atmosphere, which optionally contains a certainproportion of CO. Usually, a one-time activation of this type suffices.A presence of carbon monoxide is advantageous since it is possible totrack the course of activation through it (after successful activation,oxidation of carbon monoxide to carbon dioxide is detectable orincreased). To date, no more detailed information is availableconcerning the mechanism of activation.

One possible explanation for this activation may be that water which isfound in the pores of the foam is removed by the elevated temperature.It may also be possible that organic compounds such as hydrocarbons thatblock the surface are likewise removed by the elevated temperature. Itis also conceivable that a segregation of metals to the surface takesplace under the conditions selected for activation.

As investigations have shown, advantageous embodiments of the catalystaccording to the invention have a pore structure with diameters ofroughly 30 to 100 nm (determined with scanning electron microscopy) anda surface in the range of 2 to 8 m²/g determined with the BET process.

The plastic properties of the starting alloy make it possible,advantageously, that the alloy can even be shaped in a thin or very thinfilm, and this thin or very thin film can then be dealloyed at leastpartially by one of the above described processes.

After the dealloying process, a porous membrane-type structure with athickness of as little as 100 nm is available, through which a medium,for example, a gas or a gas mixture or a liquid may be guided. In orderto obtain the greatest possible reactions or yields, the catalystaccording to the invention may be installed, for example, in the form ofa framed or frameless membrane-type structure (membrane catalyst) atright angles to the direction of flow of a medium.

As the inventors discovered, the catalyst according to the inventionhas, for example, an excellent capability to oxidize carbon monoxide(CO) to carbon dioxide (CO₂) and to do this at temperatures of a carbonmonoxide-containing medium, for example, a gas, a gas mixture, or aliquid, as low as about −50° C. The examples described in the followingconcern tests in which this oxidation was successfully performed in therange from roughly −20° C., through 0° C. and room temperature (+23° C.)all the way up to +50° C. Of course, it is to be expected that thisoxidation reaction is accelerated by even higher temperatures, forexample, up to approximately 150° C., using the catalyst according tothe invention. In particular, catalytically mediated oxidation at lowtemperatures seems to be especially interesting since, with it, energyand, consequently, cost can be saved.

The property of efficient oxidation of carbon monoxide to carbon dioxidealso makes the catalyst according to the invention interesting forapplication in fuel cells. In particular, with polymer electrolytemembrane fuel cells (PEM), carbon monoxide can block the anode catalyst.If a catalyst according to the invention, e.g., in the form of a framedor frameless membrane catalyst, or even in the form of a conventionalcatalyst charge is arranged upstream relative to the anode catalyst inthe gas stream, disadvantageously acting carbon monoxide can be removedfor the most part, in any case, from the gas stream by this catalystbefore it is sent on to the anode catalyst.

As already mentioned above, the catalyst according to the invention mayalso be produced in the form of a particulate catalyst, for example, inpowder form, and then be used, for instance, in the form of a catalystcharge or as a finely distributed catalyst in a reaction mixture.

For the production of the catalyst according to the invention inparticle and powder form, the material can be crushed after thedealloying process through the use of an appropriate process. This iscomparatively simple because the material has a clearly higherbrittleness after the at least partial dealloying than the startingalloy. In the crushing process, care must be taken to avoid pressureloads or to keep them as small as possible since a high pressure loadcould have a disadvantageous effect through compacting or destruction ofthe pores.

Alternatively, according to the invention, the starting alloy may alsobe produced in small particles, e.g., by dripping a corresponding meltinto a cool or cooling medium. It is likewise possible to produce smallparticles from a solid starting alloy by mechanical processing. Thesmall particles of the starting alloy can then be at least partiallydealloyed as described and developed into a catalyst according to theinvention.

The catalyst particles or powder thus obtained can then, of course, beagain formed, for example, into larger units, such as pellets, forexample, and used as such.

The present invention is described more precisely through the followingstatements. These statements are based on tests and results that havebeen performed or determined using the catalyst according to theinvention for oxidation of carbon monoxide to carbon dioxide. Theoxidation of common monoxide to carbon dioxide represents, however, onlyone of the many possible areas of application for the catalyst accordingto the invention and is thus to be understood merely as one suitablemodel system for the presentation of properties of the catalystaccording to the invention. The statements thus serve merely toillustrate properties of the catalyst according to invention and mustnot be understood such that they are in any way restrictive for therange of protection of the following claims. Moreover, the data in thisdocument concerning the composition of the catalyst according to theinvention are to be understood such that in the gold used and in the atleast one less noble metal, the usually present impurities may, ofcourse, still be present.

BRIEF DESCRIPTION OF DRAWINGS

FIG. 1 Scanning electron microscope images of the porous structureaccording to the invention at a) 1500× and b) 6000× enlargement;

FIG. 2 an XPS-overview spectrum of a gold foam according to theinvention;

FIG. 3 CO₂ yields and temperature differences with different COconcentrations at +23° C. and a flow rate of 13.3 mL/min;

FIG. 4 CO₂ yields and temperature differences with different COconcentrations at +50° C. and a flow rate of 12.8 mL/min;

FIG. 5 a comparison of the yields at +50° C. and +23° C.;

FIG. 6 CO₂ yields and temperature differences with different COconcentrations at 0° C.;

FIG. 7: CO₂ yields and temperature differences with different COconcentrations at −20° C.;

FIG. 8: long-term stability of a catalyst according to the invention

EXAMPLES

1. Presentation of Exemplary Gold Foams

First, an Au—Ag-starting alloy with 30 atom % Au was produced. Thefinished starting alloy was rolled to roughly 5 mm diameter into smallpieces of desired thickness. Then, the specimens were annealed for 24hours at 850° C. For the partial dealloying and creation of the foamstructure, the specimen underwent wet-chemical treatment. The wetchemical partial dealloying was carried out in a solution of 70% nitricacid. The specimens were placed on a porous glass plate in a beaker.Then, the acid was added such that the specimen was covered. Roughly300-μm-thick specimens were dealloyed in this manner within from one tothree days. The greater part of the silver portion was selectivelydissolved out of the specimens by the nitric acid, and nanoporous goldfoams remained. The acid was removed using a syringe and replaced withwater. This was changed out several times in order to clean remainingacid residues from the specimens. The specimens were then air dried. Thespecimens have the foam structure shown in FIG. 1.

2. Surface Analysis Using XPS

XPS-analyses were performed in a UHV apparatus from the company Omicron.The specimens were placed on a specimen plate and transferred into theapparatus. The x-ray source used is a magnesium anode from the companyOmicron. Detection took place through an energy spectrometer EA 10+ fromthe company SPECS/Leybold. The energy of the photons in thesemeasurements was 1253.6 eV. In all measurements, except those in theoverview spectrum presented in FIG. 2, the pass energy was 25 eV. Forthe overview spectrum, it was 100 eV.

3. Composition of an Exemplary Catalyst

In order to determine the composition, measurements were performed onthe one hand using atom absorption spectroscopy (AAS, from the companyZeiss). For this, the specimens were dissolved in aqua regia and theninvestigated for their silver and gold content. On the other hand, thesurface composition was determined using x-ray photoelectronspectroscopy (XPS). This process is surface sensitive and detects onlythe upper atomic layer of the material. An exemplary XPS overviewspectrum is presented in FIG. 2.

From the spectrum presented in FIG. 2, it is possible to conclude thatthe gold is present in metallic, not in ionic form. The peaks at 87.75eV and 84.1 eV can be associated with the 4f-state of metallic gold,which according to the literature should be at 87.45 eV and 83.8 eV [L.E. Davis, G. E. Muilenberg, C. D. Wagner, W. M. Riggs; Handbook X-RayPhotoelectron Spectroscopy, Perkin-Elmer Corporation 1978].

Two additional peaks can be identified in the spectrum at 373.05 eV and367.06 eV. These two peaks can be associated with the 3d-state ofmetallic silver. The surface composition can be quantitativelydetermined through the integral intensities of the gold and silverpeaks—taking into account the different effective cross-sections.

Using the ratios of the integral signal intensities of silver and gold,a silver content of 4-5 atom % was determined. It was assumed that thesilver is distributed homogeneously in the areas near the surfacedetected with the method. In contrast, using AAS, a residual silvercontent of approx. 0.5 atom % was determined. This points to anenrichment of the silver on the surface.

4. Reactor Setup for the Measurements of Carbon Monoxide Oxidation

The reactor consists of a glass cylinder with a fritte (diameter 2 cm),on which the specimen (diameter 5 mm) rests. The gas is supplied via aglass tube that surrounds the cylinder in a spiral formation to controlthe temperature of the gas. (It should be noted that with the reactorsetup described, depending on flow conditions, not all gas molecules caninteract with the specimen. The gas flow rate is regulated by two flowvolume regulators from the company Brockhorst. The regulators have amaximum flow rate of 50 mL/min synthetic air and 5.6 mL/min carbonmonoxide. The deviations of the flow volume regulators from the set flowequal ±2%. The flow volume regulators are calibrated using the bubblecounter method.

Temperature control is indirect via a silicon bath in which the reactoris located and which can be temperature controlled from −20° C. to +200°C. by thermostat from the company Haak. In the interior of the reactor,there is a nickel/chromium-nickel and anickel/chromium-nickel-nickel/chromium element. The reactor temperatureis measured by the Ni/Cr—Ni-element, whereas the Ni/Cr—Ni—Ni/Cr-elementis arranged such that one node contacts the specimen and the other hangsabove it. By means of this arrangement, it is possible to measure thetemperature difference between the specimen and the reactor. The errorof such a thermal element is 1% of the temperature difference measured.

A CO₂ Uras 3G from the company Hartmann and Braun, with which the amountof carbon dioxide is measured by volume, is connected. The carbondioxide concentration in volume and the temperature difference areoutput as a voltage signal and plotted by a chart recorder LS-52-2 ofthe company Linseis. The Uras 3G is calibrated by setting differentconcentrations of carbon monoxide in synthetic air and then detectingthem using the Uras 3G. The maximum operating range of the device is 8volume percent carbon dioxide with an instrument error of 0.5%.

5. Catalysis Using an Exemplary Catalyst at +23° C.

The following statements refer by way of example to a catalyst accordingto the invention in the form of a gold foam that was produced from anAu—Ag-starting alloy (30 atom % Au) using a wet-chemical process. Thismaterial has a pore structure with diameters of approx. 50 nm determinedusing scanning electron microscopy. The surface determined with theBET-process was approx. 4 m²/g. The residual silver content was, in theentire material of the catalyst, as described, a few atom percent(0.5-2%), with silver enriched on the surface (4-20 atom %).

After a one-time activation of the catalyst at +50° C. in a gas streamof 50 mL/min of synthetic air, that contained 4 volume % carbonmonoxide, the reaction of the carbon monoxide could be continued at roomtemperature. For this, 13 mL/min of synthetic air flowed through thetest reactor, in which the specimen lying on a ceramic fritte wasexposed to the gas stream. Carbon monoxide was mixed at differentconcentrations in the gas stream. In the range from 0.14 to 7.8 volume%, constantly increasing carbon dioxide yields could be observed. Theproduct gases were detected using a carbon-dioxide-specific gas detector(Uras 3G from the company Hartmann & Braun). In addition, it waspossible to determine the temperature difference (ΔT) between thereactor and the catalyst specimen using the thermal coupler. Since thereaction investigated (CO+½O₂-->CO₂) is an exothermic reaction, thereaction could be detected by an elevated temperature of the specimencompared to the reactor. FIG. 3 depicts both the carbon dioxide yieldsin volume % and the positive temperature differences. Both resultsclearly indicate the oxidation of carbon monoxide with the catalystused. The temperature used at the time of the tests was +23° C.

6. Catalysis Using an Exemplary Catalyst at +50° C.

When one performs the same test that was described above under 5 at atemperature of +50° C., one obtains results that are very similar tothose of the test at +23° C., as can be seen in FIG. 4. Again, the yieldof carbon dioxide increases virtually linearly with increasing carbonmonoxide concentration, and the temperature differences correlate withthe yields. In FIG. 5, the yields from the measurements at +23° C. and+50° C. are presented in a graph.

7. Catalysis Using an Exemplary Catalyst at 0° C.

In the case of measurements at 0° C. the same behavior of the catalystaccording to the invention is observed as with measurements at highertemperatures. As presented in FIG. 6, both the highest yield of 4.5volume % of carbon dioxide was measured at the highest concentration ofcarbon monoxide and the lowest yield of 0.3 volume % was measured at thelowest carbon monoxide concentration.

8. Catalysis Using an Exemplary Catalyst at −20° C.

The carbon dioxide yields at −20° C. are lower than all those mentionedat higher temperatures, as shown in FIG. 7. However, the fact that sucha high conversion is even obtained at such a low temperature isunexpected and surprising and clear evidence of the qualities of thecatalyst according to the invention.

When the yields from the measurements −20° C. are considered, they nolonger reflect the typical course of the curve that was observed withall previous measurements. In contrast to the measurements at highertemperatures, the increase is no longer linear. Although an increase inthe yield of carbon dioxide formed was always measured with themeasurements at higher temperatures with increasing carbon monoxideconcentration, this appears to no longer be the case above 4 volume % ofcarbon monoxide at −20° C.

Apparently, at a lower temperature such as −20° C. the concentration ofcarbon monoxide is not the deciding factor for the reaction speed, but adifferent factor is acting in a limiting manner.

Without intending to establish a specific explanation, it might be thatthe dissociation of the molecular oxygen under the conditions acts onthe kinetics of the reaction to determine the speed.

9. Long-Term Stability

A specimen with a weight of 29.1 mg and a residual silver content of 0.5atom % in the interior and approx. 16 atom % on the surface was firstplaced in the reactor at room temperature (ca. +20° C.) and rinsed withsynthetic air. After a few minutes, 4 volume % of carbon monoxide (CO)was mixed with the gas. The entire volume flow of the gas was 50 mL/min.Under these conditions, the catalyst was, as anticipated, inactive.After raising the temperature to +50° C., the activity of the specimenstarted immediately and even continued to increase in the followinghours. The temperature of +50° C. was maintained during the furthercourse of the experiment. The curve of the activity is shown in FIG. 8.

FIG. 8 shows the activity of the specimen as a function of time.However, it must be considered that the catalyst used here (in a reactoron laboratory scale) was a very small specimen with a weight of onlyabout 29 mg. Consequently, it must be assumed that a large part of thereaction gas flowed past the catalyst surface and could not participatein the reaction. The values presented here must, consequently, beconsidered relative and not absolute units.

The invention provides a new gold-containing catalyst with porousstructure that, with a comparatively simple method for its production,is distinguished by an outstanding suitability for catalyticacceleration and/or catalytic influence on the product selectivity ofoxidation and reduction reactions and also has adequate to outstandinglong-term stability despite the absence of support material. Thesecharacteristics make the catalyst according to the inventionparticularly suited, for example, for the oxidation and, consequently,the removal of carbon monoxide from a medium, such as a gas, a gasmixture, or a liquid.

1. Gold-containing catalyst with porous structure, prepared by a methodthat comprises the following steps: producing a starting alloy bymelting together of gold and at least one less noble metal that isselected from the group consisting of silver, copper, rhodium,palladium, and platinum; and a dealloying step comprising at leastpartial removal of the less noble metal by dissolving the at least oneless noble metal out of the starting alloy.
 2. The catalyst defined inclaim 1, comprising a ratio of gold to the less noble metal(s) in thestarting alloy is in the range from 50 atom %: 50 atom % to 10 atom %:90 atom % liegt.
 3. The catalyst defined in claim 1 or 2, comprising anAu—Ag-starting alloy, the ratio of gold to silver in the starting alloyis within the range from 45 atom %: 55 atom % to 20 atom %: 80 atom %.4. The catalyst defined in one of the preceding claims, wherein theprocess further comprises a step of homogenization, in which thestarting alloy is held for an adequate time at a temperature just belowthe melting point.
 5. The catalyst defined in one of the precedingclaims, wherein the process also comprises at least one shaping stepwith which the starting alloy is given a desired shape.
 6. The catalystdefined in claim 5, comprising the shaping of the starting alloy by atleast one of the shaping methods of pressing, stamping, rolling,bending, boring, hammering, cutting, and milling is used.
 7. Thecatalyst defined in one of claims 5 or 6, further comprising, after theat least one shaping step, a step of annealing the shaped startingalloy.
 8. The catalyst defined in one of the preceding claims,comprising the dealloying step and the creation of the porous structureoccur with the use of at least one wet-chemical and/or oneelectrochemical process.
 9. The catalyst defined in one of the precedingclaims, comprising after the dealloying step, the ratio of gold to theat least one less noble metal in the porous structure is in the rangefrom 100 atom %: 0 atom % to 95 atom %: 5 atom %, determined using AAS.10. The catalyst defined in one of the preceding claims, furthercomprising a step of activation of the material obtained after the atleast partial dealloying at a temperature of roughly +40° C. to +80° C.in an oxygen-containing atmosphere, optionally in the presence of carbonmonoxide.
 11. The catalyst defined in one of the preceding claims,comprising a pore structure with diameters of roughly 30 to 100 nmdetermined with scanning electron microscopy and a surface in the rangeof 2 to 8 m²/g determined with the BET process.
 12. The catalyst definedin one of the preceding claims comprises of a powder, pellets, or amembrane-type structure, with the membrane-type structure having athickness of as little as about 100 mm.
 13. The catalyst defined in oneof claims 1 through 12 is used in a process to accelerate and/orinfluence the product selectivity of oxidation and reduction reactions.14. The process defined in claim 13 comprises oxidation of carbonmonoxide contained in a medium to carbon dioxide.
 15. The processdefined in claim 14, wherein the temperature of the carbonmonoxide-containing medium is in the range from roughly −50° C. to +150°C.
 16. A fuel cell that contains a catalyst defined in one of claims 1through
 12. 17. The fuel cell defined in claim 16, comprises a polymerelectrolyte membrane fuel cell, preferably a low temperature polymerelectrolyte membrane fuel cell.
 18. The fuel cell defined in claim 16 or17, wherein the catalyst comprises a framed or frameless membranecatalyst or a catalyst charge that is arranged upstream relative to theanode catalyst in the gas stream.
 19. The catalyst defined in claim 5,wherein said resulting gold-containing catalyst with porous structurecontains no support structure for said gold.
 20. The catalyst defined inclaim 1, where said less noble metals are selected from the groupconsisting of silver, copper and palladium.